Vapor phase treatment of combined gasoline and water phases of synthesis product with a basic compound



April 8, 1952 H, v H555 ET AL 2,591,699

VAPOR PHASE TREATMENT OF COMBINED GASOLINE AND WATER PHASES OF SYNTHESIS PRODUCT WITH A BASIC COMPOUND Filed Nov. 14, 1949 MA w/V 4. BY j Patented Apr. 8, 1952 VAPOR PHASE TREATMENT OF COMBINED GASOLINE AND WATER PHASES OF SYN- THESIS PRODUCT WITH A BASIC COM- POUND Howard V. Hess, Beacon, and George B. Arnold,

Glenham, N. Y., and Marvin L. Drabkin, Pittsburgh, Pa., assignors to The Texas Company, New York, N. Y., a corporation of Delaware Application November 14, 1949, Serial No. 127,201

9 Claims.

This invention relates to a method for treating the product obtained by the catalytic conversion of carbon monoxide and hydrogen into synthetic fuel.

This invention is a continuation-impart of Serial No. 63,463 led December 31, 1948, which discloses a process for treating the entire liquid phase of synthesis product in the vapor state at an elevated temperature of at least 500 F. with a basic compound of an alkaline metal or of an alkaline earthl metal or mixtures thereof. Vapor phase basic treatment ofthe entire liquid product results in hydrolysis of esters to alcohols and acids and in the decarboxylation of acids either to hydrocarbons or ketones. In the subject continuation-n-part a composite consisting of the gasoline fraction and the water phase of synthesis product is subjected to vapor phase treatment with a basic compound since it has been discovered that improved results are thereby obtained.

In accordance with the method of this invention, the product obtained by the catalytic conversion of carbon monoxide and hydrogen into synthetic fuel is separated into a gas phase, a water phase and an oil phase. Advantageously, separation of the synthesis product into the aforementioned component phase is effected at an elevated temperature of about 200 to 400 F. and at a pressure of about 150 to 500 pounds per square inch. The gas phase in whole or in part is recycled to the reaction zone wherein carbon monoxide and hydrogen are converted into liquid hydrocarbons. After separation of the oil phase into a gasoline fraction having an E. P. of about 400 F. and into a gas oil fraction comprising the remainder of oil phase, the gasoline fraction is combined with the water phase. The composite of gasoline fraction and Water phase is vaporized and contacted in the vapor state at an elevated temperature of at least 590 F. with a basic compoundof an alkali metal or of an alkaline earth metal or with mixtures of such basic compounds. Treatment of the combined gasoline fraction and water phase in the vapor state with a compound selected from the aforedescribed group results in hydrolysis of water-soluble esters and oil-soluble esters boiling in the gasoline fraction to alcohols and acids and in decarboxylation of water-soluble acids and oil-soluble acids boiling in the gasoline range either to hydrocarbons or ketones. After contacting the combined gasoline fraction and water phase in the vapor state with a basic compound, the composite is cooled and separated into e gaseous fraction, a water phase and a gasoline phase.

The gaseous fraction obtained on cooling and separation of the base-treated composite is recycled in whole or in part to the reaction zone wherein carbon monoxide and hydrogen are converted into synthetic fuel. As an alternative procedure, this gaseous fraction can be sent to a poly plant for polymerization into higher molecular Weight hydrocarbons. Aqueous azeotropes of alcohols, ketones and hydrocarbons are separated from the water phase; ilashing provides a convenient method for removing aqueous azeotropes from the water phase. The gasoline fraction is readily freed from oxygenates which are mainly in the formof alcohols by solvent extraction or silica gel adsorption.

Catalytic conversion of carbon monoxide and hydrogen into synthetic fuel by contact with a uidized iron catalyst at an elevated tempera- -ture of 500 to 750 F. and at a pressure of 100 to 500 pounds per square inch results in the formation of a product comprising a gas phase and a liquid phase, the latter consisting of approximately one part oil phase and 2 parts Water phase. Oxygen-containing organic compounds, such as,

alcohols, acids, esters, ketones, and aldehydesare distributed throughout the two phase liquid product; the molecular weight of the oxygen-contaming compounds determines whether they are primarily found in the water phase or in the-oil phase. The oxygen-containing organic compounds ordinarily found in the water phase comprise lower molecular weight compounds, such as, C1 to Ce alcohols, esters containing up to about 4 carbon atoms and C2 to Cs organic acids with traces of the higher molecular weight compounds. The oxygen-containing organic compounds ordinarily found in the oil phase comprise higher molecular weight compounds, such as, C4 and higher alcohols, esters containing more than 3 carbon atoms and C3 and and higher organic acids with traces of the lower molecular weight compounds. It will be noted that there is considerable overlapping in the distribution of the oxygen-containing compound between the oil and water phases. This overlapping is due to the fact that compounds of intermediate molecular weights, such as, C5 alcohols are found in substantial proportion in both oil and water phases.

The disposal of the water phase in large scale commercial operation poses a serious problem since the oxygen-containing organic compounds comprise as high as 20 per cent of the water phase and their presence therein would seriously pollute any stream or river into which the water phase is dumped. The oxygen-containing organic compounds present in both theY oil and water phases are valuable chemicals in their own right and are in high demand as chemicals of commerce. The subject invention provides a method for expediting the recovery of oxygencontaining organic compounds from both the oil and Water phases and also puries the Water phase to such an extent that it can be poured into rivers and streams without fear of polluting them.

The liquid product, consisting of oil and water phases, obtained by the catalytic conversion o carbon monoxide and hydrogen into liquid hydrocarbons by contact With a iluidized iron catalyst at an elevated temperature of 500 to 750 F. and at a pressure of 100 to 500 pounds per square inch contains approximately to 25 per cent oxygen-containing organic compounds. The distribution of the various types of oxygen-containing organic compounds in this 15 to 25 per cent fraction of product is best illustrated by considering the concentration of the oxygen-containing organic compounds in the oil and Water phases obtained by separation of the liquid product at atmospheric conditions. The aqueous 'phase separated from the liquid phase at atmospheric conditions contains approximately per cent oxygen-containing organic compounds which are distributed among the various oxygencontaining organic compounds approximately as follows: l2 per cent alcohols, 3 per cent acids,3 per cent esters, 1 per cent aldehydes, 1 per cent ketones. The oil phase separated from the liquid product at atmospheric conditions, contains approximately 13 per cent oxygen-containing organic compounds which are distributed among the various types of organic compounds as follows: 7 per cent alcohols, 2 per cent acids, 2 per cent esters, l per cent aldehydes, and 1 per cent ketones. It will be noted that alcohols form the major portion of the oxygen-containing organic compounds in both the Water and oil phases', acids and esters are also present in the cil and Water phases in a substantial portion, whereas aldehydes and ketones constitute a relatively small fraction of both the Water and oil phases.

The gasoline fraction having an E. P. of 400 F., Which is obtained by separation of the synthesis product into oil and Water phases at a temper-a- Yture between 200 and 400 F. and a pressure of from 150 to 500 pounds per square inch and by fractionation of the oil phase so obtained into a gasoline fraction having an E, P. of 400 F'. and a residu-al gas oil fraction, contains approximatelly 6 per cent alcohols, 3 per cent acids, 5 per cent esters, 1 per cent aldehydes and 1 per cent ketones. i

Treatment of the combined gasoline fraction and oil phase at an elevated temperaturev in the vapor state with a basic compound and the type previously described, hydrolyzes esters to alcohols and acids and dicarboxylates acids initially present and acids formed by ester hydrolysis. Water- `soluble esters and oil-soluble esters boiling in the gasoline range are both efficiency hydrolyzed.

-In similar fashion, both Water-soluble acids and -oil-soluble acids boiling up to 400 F. are decarboxylated with about equal eiciency. Watersoluble alcohols and ketones and oil-soluble alcohols and ketones boiling up to about 400F. are

substantially unaffected by vapor. phase treatment with the basic compound of the aforedescribed conditions. Water-soluble and oil-soluble aldehydes are polymerized to high molecular weight materials which undergo cracking underl the conditions of reaction.

An outstanding feature of the subject invention is that hydrolysis of water-soluble and oilsoluble esters is effected in the vapor state. The Vapor phase hydrolysis of oil-soluble and Watersoluble esters at elevated temperatures over solid basic compounds of the type hereinbefore described, is a surprising and advantageous result of the process of the subject invention.

Another outstanding advantage of the subject invention resides in the fact that the water phase, after separation from the base-treated liquid product and after removal of aqueous azeotropes of the low molecular Weight alcohols, ketones and hydrocarbons therefrom, is practically free from acids and other oxygen-containing organic compounds. Consequently, disposal of the Water phase does not present a problem since it may be emptied into a river or a stream Without fear of causing pollution.

A third advantage of the subject invention results from,V the fact that a high recovery of oxygen-containing organic compounds in the form of alcohols and ketones is realized.

Alkali metal hydroxides, alkali metal oxides, alkali metal salts, alkaline earth metal hydroxides, alkaline earth metal oxides, alkaline earth metal salts and mixtures thereof are included among the basic compounds Which can be employed to eiect vapor phase base-treatment of the liquid product obtained by the conversion of carbon monoxide and hydrogen into synthetic fuel. Alkali metals are monovalent elements of the first group of the periodic system; examples are sodium, potassium, lithium, etc.; alkaline earth metals are-divalent elements of the second group of the periodic system; examples are calcium, barium, strontium, and the like. Both alkali metal compounds and alkaline earth metal compounds effect vapor phase hydrolysis of oilsoluble and Water-soluble esters to alcohols and acids. Basic alkali metal compounds and basic mixtures of alkaline earth and alkali metal compounds decarboxylate oil-soluble and Water-soluble acids formed by ester hydrolysis and oil-soluble and water-soluble acids initially present in the liquid product mainly to hydrocarbons; on the other hand, basic alkaline earth metal compounds decarboxylate acids mainly to ketones.

While both basic alkali metal compounds and basic alkaline earth metal compounds effect decarboxylation of acids and yhydrolysis of esters in the liquid product and a high degree of the clarication of the water phase of the liquid product, the alkali metal group or mixtures containing alkali metal group of compounds are preferred because they are more eicient. A quicker and more complete treatment of the liquid product can be eiected with basic alkali metal compounds than with basic alkaline earth metal compounds. As a Consequence, a larger quantity of liquid product can be treated in a unit of time with alkali metal compounds than with alkaline earth metal compounds. Sodium carbonate, sodium phosphate, potassium carbonate, potassium phosphate, potassium borate, sodium hydroxide and potassium hydroxide are examples of basic alkali metal compounds which can be employed in the process of this invention. Sodium carbonate and sodium phosphate are particularly preferred compounds for use in the method of this invention; not only are these compounds particularly active in effecting hydrolysis of esters and decarboxylation of acids, but they are also inexpensive chemicals. Calcium oxide, calcium carbonate, barium oxide, barium carbonvadvantage of effecting separation of synthesis product at elevated temperature and pressure resides in the saving in power requirements thereby realized. There is realized a saving in the heat required to fractionate the oil phase into a gasoline fraction and a gas oil fraction and substantial savings are effected in the heat required tovaporize the combined gasoline fraction and water phase. However, the process of this invention is also applicable to a synthesis product, which has been separated into gas, Water and oil phases at atmospheric conditions.

The oil phase is fractionated into a gasoline fraction and a residual gas oil fraction after separation of the synthesis product into gas, water and oil phases. Division of the oil phase into gasolineand gas oil fractions can be made at a temperature varying between 350 and 400 F. Advantageously, however, the fractionation is conducted to give a 400 F. E. P. gasoline fraction.

Contacting of the combined gasoline fraction and water phase with a basic material is effected at a temperature between 500 and 1000 F.; it has been found that temperatures between '700 and 950 F. are preferred. It is advisable to employ temperatures inthe upper part of the separating range, that is, temperatures of 800 to 1000o F. with alkaline earth metal compounds, whereas temperatures between 700 and 900 F. are advantageous with an alkali metal compound.

Pressures ranging from atmospheric to about 500 pounds per square inch may be employed forthe basic treatment of the composite. At-

-inospheric pressure is ordinarily employed although the use of higher pressures results in smaller equipment. The composite consisting of gasoline fraction and water phase is contacted with a basic compound at a space velocity between about 1 and 10 volumes of liquid product per volume of solid basic material per hour. Space velocities betweenvabout 2 and 5 arev preferred. IAs a general proposition, higherspace velocities may be employed with alkali metal compounds than with alkaline earth metal compounds.

It is possible to effect the vapor phase contacting. of the composite in accordancel with "any of the usual techniques for catalytic vvapor `phase contacting. Accordingly, the combinedV gasoline 'fraction and aqueous phase can bepassed inthe Avapor state through a. fixed b'ed of solid basic material maintained at a temperature between `500 and 1000 F. or canbe contacted withfa 7 5;

iluidized bed of "basic material particles. The

vvaporized compositecan also be contacted .with

a, moving bed of basic material particles. or with astirred bed of basic material particles.

After treatment with a basic material at a temperature between 500`and 700 F. the combinedlgasoline fraction and water phase 'is condensed and'separated into a gaseous fractioma Water phase and a gasoline fraction. This separationv is also advantageously effected at an elevated'temperature of from 200to 400 F. and a pressure of from 150 to l500 pounds per square inch. As was indicated previously, non-acidicV normally water-soluble oxygen-containing orfganic compounds are displaced from thefwater phase into the oil phase by-such elevated temvperature and pressure separation. Water-solublefoxygenated compounds which are predominantly-in the form of alcohols after basic'treat'- mentare displaced from the water phase tothe gasoline fraction by elevated temperature and pressureseparation. The advantage of such displacement is that the oxygenate content offthe water phase is reduced so that it is easier to ob- '.tain a rejectable water by flashing oxygenates therefrom in the form of aqueous azeotropes.

After alcohols and ketones have been'separated from the water phase in the form of aqueous azeotropes, the water phase contains less than 0.2 per cent oxygen-containing organic compounds `and may be introduced into a river or streamfor disposal without fear of polluting them. The gaseous fraction which comprises mainly gaseous hydrocarbons such as ethane, ethylene, propane, etc., and which is of relatively small volume, only l kcomprising up to 4.0 weight per `cent of baseltreated liquid product, is advantageously recycled "'-to the reaction zone wherein hydrogen and'ca'r- 'bonl monoxide are converted binto syntheticfuel. vAlcohols and ketones are readily separated-from the gasoline fractionby solvent extraction with a f solvent, such as, aqueous methanol, ethylene glycol,.diethylene` glycol, propylene'glycol, furfural, etc. Silica gel adsorption may also be'emjployed to separate alcohols and ketones from the gasoline fraction, but it is ordinarily not employed crease in alcohol content and substantial decrease in acid andester content of both the gasoline :fraction and water phase after treatment with sodium carbonate at a4 temperature of approximately 900 F. The gasoline fraction, after 'separation from the liquid product at atmospheric conditions, had an alcohol content of 4 volume percent, an acid content of 3 volume percent and an ester contentof 4 volume per cent with minor l amounts of aldehydes and ketones whereas the water `phase separated from the composite at Vatmospheric conditions, had an alcohol content a of' A12-volume per cent, an acid content of 2 volume A cent.

percent and an ester content of 3 volume per' After` the composite comprising gasoline l fraction and water phase was contacted with -a vfixed bed of sodium carbonate at a temperature of about 900 F., a space velocity of 2 volumes of 7.0v-

liquid product per volume of 'solid basic comf `pound per hour and after `separation'of the rbasetreated composite into gasoline fraction 'and l water phase at atmospheric conditions. the gasoline fraction had an alcohol content of 7 volume percent, an acid content of less than 1 volume per cent, and an ester content of less than 1 volume per cent; after the aforementioned treatment the water phase had an alcohol content oi 13 volume per cent, an -acid content of less than 1 volume per cent, rand an ester content of less 1 volume per cent. The decrease in the acid and ester contents of both phases are significant. As

v,has been indicated previously, alcohols and ketones. are readily removed from the water phase in the form of aqueous azeotropes by hashing.

In the accompanying igure, there is presented a ow diagram wherein the process of the subject invention is described in detail.

, Hydrogen and carbon monoxide are introduced -through a pipe I into a synthesis reactor 2 wherein conversion of carbon monoxide and hydrogen into liquid hydrocarbons is effected by contact with an iron catalyst maintained in a fluid state at a temperature between 500 and '700 F. and of Ya. pressure between 150 and 500 pounds per square inch.

An eluent comprising unconverted hydrogen .and carbon monoxide, carbon dioxide and products of reaction comprising water, gaseous and liquid hydrocarbons, oxygen-containing organic compounds issues from the reactor 2 through a pipe 3 and is introduced into a heat exchange 4 ,wherein the product is cooled to a temperature between 150 and 400 F. and preferably between a temperature between 200 and 300 F. with no .reduction in pressure. Thereafter, the eiiiuent v.is introduced through a pipe 5 to a separator 1 Imaintained at a temperature between 150 and *400 F. and preferably between 200 to 300 F. and

a pressure between 150 and 500 pounds per square inch. Advantageously, the separator ismain- -tained at approximately the same Tpressure that is. employed for the conversion of carbon monoxide and hydrogen in the reactor 2. In the separator 'I the etiluent is separated into a gas phase, a water phase and an oil phase.

. Separation of a synthesis product into a gas phase, an oil phase and a water phase at elevated temperature and pressure relieves the load on `heat exchange facilities, since the oil phase is .immediately converted into a gasoline fraction arid a gas oil fraction andthe aqueous. phase after combination with the gasoline fraction is raised to a temperature of 500 to 1000 F.

.The gas phase is withdrawn from the separator I through a pipe 9 through which it is recycled to the synthesis reactor 2 so that a recycle ratio of .recycle gas to fresh feed between about 1 to 1 and 5 to 1 is maintained. A drawoi pipe I0 affords means of withdrawing that portion of the g'as phase which is not recycled.

` 'The oil phase is withdrawn from theseparator `I through a Apipe II and is introduced into a jiractionating tower I2 wherein the oil phase is separated into a gasoline fraction and a residual Vgas oil fraction by fraction distillation. Division of the oil phase into gasoline fraction and a gas Water phase is withdrawn from the separator 1 through a pipe I6 and combines with the gasoline fraction flowing through the pipe I3.

The composite of water phase and gasoline fraction is raised to a temperature between 500 and 1000o F. in the heat exchanger I8 and is thereafter introduced i-nto a base treater 20 through a pipe I9;

'ebase treater 20 contains a basic material of the type heretofore described and is maintained at a temperature between 500 and 1000 F. and at atmospheric pressure.

The combined gasoline fraction and water phase contacts in the base treater 20 a basic compound of analkali metal, anA alkaline earth metal or a mixture of such compounds. For purposes of description; it will be assumed that the base treater 20 contains an alkali metal salt such as sodium carbonate. The `basic treatment of the composite in the vapor state with sodium carbonate hydrolyzes the esters to alcohols and acids and decarboxyiates the acids-initially present together with those formed by ester hydrolysis to hydrocarbons.

The water-soluble and oil-soluble aldehydes are polymerizedby vapor phase contacting with sodium carbonate to high molecular weight compounds which are partially-cracked to smaller molecular weight hydrocarbons. The oil-soluble and water-soluble alcohols and ketones are substantiaily unaiected with theexception that the alcohol content is substantially increased by ester hydrolysis.

The base-treated composite with its acid, ester and aldehyde content substantially reduced but with an increased content of alcohols and hydrocarbons, is introduced through a pipe 23 into heat exchanger-26 wherein it is cooled to a temperature between and 400 F. and preferably to approximately 250 F. The base-treated com'- posite is then introduced through a pipe 2l into a separator 30 wherein it is separated into a gaseous fraction, a gasoline fraction and a water --phase at elevated temperature and pressure. v

Separation of the base-treated composite into a gasoline fraction and water phase at an elevated pressure between 150 and 500 pounds per square inch and at an elevated temperature of 150 to- 400 F. eiects displacement of alcohols and ketones normally soluble in the water phase into the oil phase. The gaseous fraction comprising a relatively small amount of gaseous hydrocarbons.such as, ethane, butenes, butanes, etc., is withdrawn from the separator 30. through4 a pipe 3l through which it is recycled to the reaction zone. The pipe 3l leads into the pipe I through which the gas phase originally separated from the synthesisv product is recycled to the synthesis reactor 2.

The gasoline fraction is withdrawn from the separator 30 through a pipe 33. Oxygenated compounds, which are predominantly alcohols,

although there are -minor portions of vlxetones present inthe gasoline fraction, are simply extracted from the gasoline fraction with a gasoline-immiscible solvent, such as aqueous methanol, ethylene glycol, poly glycols, and cfurfural.

The gasoline fraction obtained in the aforedescribed manner has an alcohol content of '7 volume per cent, a combined acid and ester content of less than 1 volume per cent and a ketone content of l volume per cent. The high alcohol content and the low ester and acid contents of the gasoline fractionare signicant.

- The water phase is withdrawn from the separator 30 :through 'a pipe 40 andis introduced therethrough to a iiash tower 4I. Aqueous azeo- -tropes of alcohols, ket'ones and hydrocarbonsare removed from the flash tower 4I through a pipe 42. .Thereafteig the azeotropes may be further .separatedv into individual constituents. j Thereject Water obtained from the flash tower 4I through a draw-off pipe 43 has an alcohol content less than 1.0 volume per cent, and a combined acid and ester content of less than 1 Volume per cent. The Water phase thus substantially rfree from organic compounds, may be rejected through the pipe 43 and poured into a nearby body of Water without danger of polluting same.

It will be understood that the foregoing detailed description is merely illustrative of the process of the invention and is not intended as any limitation thereon. The synthesis product can be cooled and separated into a gas phase, a Water phase and an oil phase at atmospheric conditions rather than at elevated temperature and pressure in the detailed description prior to contacting the combined gasoline fraction and Water phase in the vapor phase with a basic compound. Moreover, it is also possible to separate the basetreated composite into a gaseous fraction, a Water phase and a gasoline fraction at atmospheric conditions rather than at elevated temperature and superatmospheric pressure as in the detailed description.

As has been indicated previously, a basic alkaline earth metal compound, such as calcium oxide, or mixtures of basic alkali metal compounds and alkaline earth metal compounds can be employed for the vapor phase treatment of the liquid synthesis product. The use of a basic alkaline earth metal compound increases the ketone content of the liquid product by decarboxylation of acids to ketones.

Obviously, many modications and variations of the invention as hereinbefore set forth may be made without departing from the spirit and scope thereof, and therefore only such limitations should be imposed as are indicated in the appended claims.

We claim:

l. A process for treating a product containing water, hydrocarbons and oxygen-containing organic compounds comprising alcohols, esters, acids, aldehydes and ketones, and which is obtained by the catalytic conversion of carbon monoxide and hydrogen into synthetic fuel, which comprises separating said product into a gas phase, a Water phase and an oil phase, fractionating said oil phase into a gasoline fraction and a gas oil fraction, combining said Water phase with said gasoline fraction to form a composite phase consisting of said gasoline fraction and said Water phase vaporizing said composite phase, contacting said composite in the vapor state at a temperature of 500 to 1000 F. with a solid basic material selected from the group consisting of alkali metal compounds, alkaline earth compounds and mixtures thereof whereby esters are hydrolyzed and acids are decarboxylated, separating said composite into a gaseous fraction, a Water phase and a gasoline fraction, separately removing alcohols and ketones from said water phase and said gasoline fraction.

2. A process according to claim 1 in which the composite is contacted with a basic material at a temperature of 700 to 950 F.

3. A process according to claim 1 in Which the catalytic conversion of carbon monoxide and f hydrogen into synthetic fuel is eiected by contact with an iron catalyst at a temperature of about 500 to 700 F. and at a pressure of from to 500 pounds per square inch.

4. A process according to claim 1 in which the vaporized composite is contacted in the vapor state with a basic alkali metal compound.

5. A process according to claim 1 in which the vaporized composite is contacted With sodium carbonate.

6. A p rocess according tol claim 1 in which the separation of synthesis product into a gas phase, a water phase and an oil phase is effected at a temperature of about to 400 F. and at elevated pressure.

7. A process according to claim 1 in which the base-treated composite is separated into a gaseous fraction, a Water fraction and a gasoline fraction at an elevated temperature of 150 to 400 F. and at elevated pressure.

8. A process according to claim 1 in which the base-treated composite is separated into a gaseous fraction, a water fraction anda gasoline at atmospheric conditions.

9. A process according to claim 1 in which the gaseous fraction separated from the base-treated composite is recycled to the synthesis reaction.

HOWARD V. HESS. GEORGE B. ARNOLD. MARVIN L. DRABKIN.

REFERENCES CITED The following references are of record in the iile of this patent:

UNITED STATES PATENTS Number Name Date 1,979,303 Woodhouse Nov. 6, 1934 2,076,607 Woodhouse Apr. 13, 1937 2,452,121 Grahame Oct. 26, 1948 

1. A PROCESS FOR TREATING A PRODUCT CONTAINING WATER, HYDROCARBONS AND OXYGEN-CONTAINING ORGANIC COMPOUNDS COMPRISING ALCOHOL, ESTERS, ACIDS, ALDEHYDES AND KETONES, AND WHICH IS OBTAINED BY THE CATALYTIC CONVERSION OF CARBON MONOXIDE AND HYDROGEN INTO SYNTHETIC FUEL, WHICH COMPRISES SEPARATING SAID PRODUCT INTO A GAS PHASE, A WATER PHASE AND AN OIL PHASE, FRACTIONATING SAID OIL PHASE INTO A GASOLINE FRACTION SAID A GAS OIL FRACTION, COMBINING SAID WATER PHASE WITH SAID GASOLINE FRACTION TO FORM A COMPOSITE PHASE CONSISTING OF SAID GASOLINE FRACTION AND SAID WATER PHASE VAPORIZING SADI COMPOSITE PHASE, CONTACTING SAID COMPOSITE IN THE VAPOR STATE AT A TEMPERATURE OF 500 TO 1000* F. WITH A SOLID BASIC MATERIAL SELECTED FROM THE GROUP CONSISTING OF ALKALI METAL COMPOUNDS, ALKALINE EARTH COMPOUNDS AND MIXTURES THEREOF WHEREBY ESTERS ARE HYDROLYZED AND ACIDS ARE DECARBOXYLATED, SEPARATING SAID COMPOSITE INTO A GASEOUS FRACTION, A WATER PHASE AND A GASOLINE FRACTION. SEPARTELY REMOVING ALCOHOLS AND KETONES FROM SAID WATER PHASE AND SAID GASOLINE FRACTION. 